JPH05203286A - Heat exchanger - Google Patents

Abstract

PURPOSE:To provide a heat exchanger which is equipped with a flow divider which divides the flow of refrigerant in a two phase state (vapor and liquid) among a plurality of refrigerant circuit and capable of heat exchanging with high efficiency by dividing the refrigerant among the refrigerant circuits equally in terms of a refrigeration cycle of refrigerator or air conditioner. CONSTITUTION:This heat exchanger comprises a cylinder shaped flow divider 12, a cylinder-shaped flow combiner 13, heat exchanger tubes 14 to the flow divider 12 and the low combiner 13 and a large number of fins 15 installed to the heat exchanger tubes. A turbulent flow promoter 18 is installed inside the flow divider 14. Therefore, this heat exchanger comprises the flow divider and the flow combiner which are cylinder-shaped and sealed on both ends, a plurality of heat exchanger tubes welded to the flow divider and the flow combiner virtually at right angles and the fins installed in great numbers. The turbulent flow promoter is installed inside the flow divider as well. The liquid refrigerant can flow out to the flow divider welded to the heat exchanger tubes substantially equally, thereby carrying out a heat exchange performance with a high efficiency.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a heat exchanger having a flow divider used as a header pipe in an evaporator such as a refrigerating machine or an air conditioner.

[0002]

2. Description of the Related Art In recent years, header pipes and the like have been used as shunts in order to meet the demand for smaller diameter and higher efficiency of heat transfer tubes in response to the demand for miniaturization and high efficiency of heat exchangers (for example, actual shunts) 63-173689).

An example of the conventional heat exchanger described above will be described below with reference to the drawings. FIG. 9 shows a perspective view of a conventional heat exchanger. Reference numeral 1 is a heat exchanger, and a plurality of heat transfer tubes 4 are joined to cylindrical flow distributors 2 and 3 whose both ends are sealed,
A plurality of fins 5 are arranged in the heat transfer tube 4. Shunt 2
An inlet pipe 6 and an outlet pipe 7 are attached to the heat exchanger, and the flow dividers 2 and 3 are provided with partitions 2a, 2b, and 3a, and the heat transfer pipe 4 constitutes a refrigerant circuit.

The operation of the heat exchanger configured as described above when used as an evaporator will be described below with reference to the drawings.

In FIG. 9, the refrigerant R in the gas-liquid two-phase state flowing from the inlet pipe 6 into the compartment 2A of the flow divider 2 is divided into the partition 2a.
The heat is divided into a plurality of lower heat transfer tubes 4 and discharged. The refrigerant R is provided with a large number of fins 5 arranged in the heat transfer tube 4.
Through the heat exchanger 1 and the air A flowing in from the entire surface of the heat exchanger 1 to be evaporated and flow into the compartment 3A of the flow divider 3. The refrigerant R merged in the flow divider 3 flows upward in the flow divider 3 and is distributed to the plurality of heat transfer tubes 4 below the partition 3a and flows out. Similarly, the refrigerant R, which is evaporated while repeating merging and distribution in the flow divider 23, becomes dry vapor and merges in the section 2C above the partition 2b, flows out from the outlet pipe 7 attached to the flow divider 2.

10 and 11 are vertical cross-sectional views of the flow dividers 2 and 3, showing how the refrigerant R flows, and the arrows in the figures indicate the direction of the refrigerant R flow. The gas-liquid two-phase refrigerant R flowing in from the inlet pipe 6 evaporates in the heat exchanger 1,
The degree of dryness is gradually increased and the split flow is repeated to form dry steam, which flows out from the outlet pipe 7.

[0007]

However, in the above configuration, as shown in FIGS. 10 and 11, the dryness increases in the sections 2A to 2C and 3A to 3B in the flow dividers 2 and 3, respectively. In addition, the flow pattern changes from the froth flow to the annular spray flow. In the vertical upward gas-liquid two-phase flow, when the dryness is small, it becomes a froth flow, and when the dryness increases, it becomes an annular spray flow. For example, the flow pattern of vertical upward flow shown in Fig. 12 (Opportunity Engineering Handbook, Basic Edition, A5 Fluid Dynamics, published by The Japan Opportunity Society (19)
86) According to A5-Page 153), Freon R22 (pressure 0.7M), which is generally used for refrigerant R, is used for air conditioning.
Pa), the flow pattern of the refrigerant R is such that the dryness is 0.2.
Is the point on the line L1, and when the dryness is 0.6, the line L2
It becomes the upper point. Here, the dryness of 0.2 is the state of the refrigerant R at the inlet of the heat exchanger for evaporation of a general refrigeration cycle,
The dryness of 0.6 is the state of the intermediate refrigerant until reaching the outlet. Points P1 and P2 are points when the refrigerant R of each dryness has the same mass flow rate, and even when the refrigerant R has the same mass flow rate, the larger the dryness is, the more likely the annular spray flow is. The points P1 and P2 move downward on the lines L1 and L2 as the flow rate of the refrigerant R decreases due to the decrease in the mass flow rate of the refrigerant R, and the apparent flow rates of the gas phase and liquid phase of the refrigerant R decrease. .. As described above, even if the refrigerant R has the same mass flow rate, in the sections 3B and 2C near the outlet pipe 7 having a high degree of dryness, after the refrigerant R merges, an annular spray flow is likely to occur.

Further, the sections 3B and 2C having an annular spray flow.
Then, the refrigerant R sequentially flows out to the heat transfer tube 4 while flowing upward, so that the mass flow rate of the refrigerant R in the flow dividers 2 and 3 decreases,
The apparent flow velocities of the refrigerant R in the gas phase and the liquid phase become slower, as shown in FIG.
At, it will move downwards and eventually move to the froth flow.

In the case where the gas-liquid two-phase flow splits, the fact that the flow mode greatly affects the split flow ratio is, for example, a study on the gas-liquid two-phase flow behavior from the horizontal pipe to the vertical branch pipe (first Report) (1991-5) Proceedings of 28th Japan Heat Transfer Symposium, pp. 766-768, Fig. 1
As shown in Fig. 3, the refrigerant R is present in the annular spray basin and the floss basin.
It is known that the flow ratios of the refrigerant R are largely different and the liquid phase of the refrigerant R is more likely to flow out in the froth flow.

From the above, the liquid phase of the refrigerant R is different in each of the sections 2A and 3A immediately after the refrigerant R flows into the heat exchanger 1 and the degree of dryness is likely to cause a froth flow in all regions. The flow is evenly distributed to the heat transfer tube 4. However, the compartments 2B, 3 into which the refrigerant R flows after evaporating to some extent in the heat exchanger 1
In B, since the dryness is large, an annular spray flow is likely to occur at first. However, the refrigerant R sequentially flows out into the heat transfer tubes 4 while flowing upward in the sections 2B and 3B, so that the mass flow rate decreases and the refrigerant flows to the froth flow.

Therefore, the liquid phase of the refrigerant R is less likely to flow out from the upper part where the lower part which is the annular spray flow becomes the froth flow, and almost the gas phase of the refrigerant R flows into the heat transfer tube 4 joined to this part. And almost no evaporation occurs, and the amount of heat exchange is very small. In addition, the refrigerant R in all the flow dividers 2 and 3
If the diameters of the cylindrical flow distributors 2 and 3 are made sufficiently large in order to make the floss flow, it is necessary to make the diameter very large especially for the flow distributors 2 and 3 near the outlet where the dryness is high. The first problem is that the volume of the heat exchanger 1 becomes very large due to the portions that do not directly perform heat exchange, that is, the flow dividers 2 and 3, and the demand for miniaturization of the heat exchanger 1 cannot be met. Had.

Therefore, the present invention has a flow divider that evenly distributes the refrigerant to each heat transfer tube when used as an evaporator,
It is intended to provide a compact and high-performance heat exchanger.

[0013]

In order to solve the above problems, a heat exchanger according to the present invention comprises a tubular flow distributor whose both ends are sealed, and a tubular flow combiner whose both ends are sealed. A turbulence promoting body is provided inside the shunt, which is composed of a plurality of heat transfer tubes joined to the shunt and the merger at substantially right angles, and a plurality of heat transfer fins arranged on the heat transfer tube. It has a configuration.

In order to solve the above-mentioned problems, the heat exchanger of the present invention is a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, the above-mentioned flow distributor, and the above-mentioned flow divider. A configuration in which a ribbon-shaped turbulence promoting body is provided inside the flow distributor, which is composed of a plurality of heat transfer tubes joined at substantially right angles to the confluencer and a plurality of heat transfer fins arranged in the heat transfer tube. Be prepared.

In order to solve the above-mentioned problems, the heat exchanger of the present invention is a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, the above-mentioned flow distributor and the above-mentioned flow distributor. A plurality of heat transfer tubes joined at substantially right angles to the confluencer, and a plurality of heat transfer fins arranged on the heat transfer tube. A ribbon-shaped turbulence promoting body is provided inside the flow distributor at the bottom of the flow distributor. From to the top,
It has a configuration that it is provided in almost the entire area.

In order to solve the above-mentioned problems, the heat exchanger of the present invention comprises a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, said flow distributor and said A plurality of heat transfer tubes joined at substantially right angles to the confluencer, and a plurality of heat transfer fins arranged on the heat transfer tube. A ribbon-shaped turbulence promoting body is provided inside the flow distributor at the bottom of the flow distributor. It is provided with a configuration that is provided only in.

In order to solve the above-mentioned problems, the heat exchanger of the present invention is a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, the above-mentioned flow distributor and the above-mentioned flow distributor. A structure in which a turbulent flow promoting body having small holes is provided inside the flow distributor, which is composed of a plurality of heat transfer tubes joined at substantially right angles to the confluencer and a plurality of heat transfer fins arranged in the heat transfer tube. It is equipped with.

[0018]

According to the present invention, with the above-described structure, the flow mode is changed to the froth flow by the turbulence promoting body in the portion of the annular spray flow having a high degree of dryness, and the liquid refrigerant is all heat transfer tubes connected to the flow divider. The liquid-phase refrigerant flows out into the heat transfer tubes almost uniformly, and evaporation is similarly performed in all the heat transfer tubes, so that heat exchange is efficiently performed.

Further, according to the present invention, the turbulence promoting body is ribbon-shaped, the annular spray flow is efficiently converted to the froth flow, and the liquid refrigerant is transferred to all the flow distributors connected to the flow divider. It evenly flows out to the heat pipe, evaporation is performed in the same manner, and heat exchange is efficiently performed.

Further, according to the present invention, the turbulent flow promoting body is provided in the entire region from the lower part to the upper part of the flow diverter with the above-mentioned constitution, so that the flow mode is the froth flow in the part of the annular spray flow having a high dryness in the lower part. And the mixing of the refrigerant is promoted also in the upper froth flow region. Therefore, the liquid refrigerant is
It evenly flows out to all the heat transfer tubes connected to the flow divider, and evaporation is similarly performed in all the heat transfer tubes to efficiently perform heat exchange.

Further, according to the present invention, the ribbon-like turbulence promoting body is provided only in the lower portion, which is the portion of the annular spray flow having a high degree of dryness, by the above-mentioned constitution, and the material is effectively utilized. The part of the annular spray flow moves to the floss flow, and the liquid refrigerant
It evenly flows out to all the heat transfer tubes connected to the flow divider, and evaporation is similarly performed in all the heat transfer tubes to efficiently perform heat exchange.

Further, according to the present invention, the turbulent flow promoting body having the small holes is provided in the flow distributor with the above-mentioned configuration, and the portion of the annular spray flow is transferred to the floss flow.
The refrigerant that passes through the small holes and the refrigerant that does not pass through the small holes are mixed, and the liquid refrigerant evenly flows out to all the heat transfer tubes connected to the flow divider, so that heat exchange is efficiently performed.

[0023]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below with reference to the drawings.

FIG. 1 is a perspective view of a heat exchanger according to the first embodiment of the present invention. Reference numeral 11 denotes a heat exchanger, and a plurality of heat transfer tubes 13 are joined in a row to a tubular flow distributor 12 whose both ends are sealed. Further, a plurality of heat transfer tubes 13 are joined in one row also to the confluencers 14 arranged in parallel, the heat transfer tubes 13 are installed in two rows, and a large number of fins 15 are arranged. The heat transfer tube 13 joined to the flow divider 12 is appropriately connected in a U shape, and the refrigerant R
1 circuit is formed. The flow divider 12 has an inlet pipe 16
And the outlet pipe 17 is joined to the confluencer 14. A ribbon-shaped turbulence promoting body 18 as shown in FIG. 2 is provided inside the flow distributor 12 in almost the entire region from the upper part to the lower part of the flow distributor 12.

The operation of the heat exchanger 11 configured as described above will be described below with reference to FIGS. 1 and 3.

The gas-liquid two-phase refrigerant R1 having a low degree of dryness sequentially flows out to the heat transfer tube 13 while flowing upward in the flow divider 12 flowing into the flow divider 12 from the inlet pipe 16. U as appropriate
The heat transfer tube 13 on the rear surface side of the heat exchanger 11 evaporates while exchanging heat with the air A1 flowing from the entire surface on the side of the flow divider 12 via the fins 15 arranged on the heat transfer tube 13 connected in a letter shape.
After it becomes dry steam, it reaches the confluencer 14, merges, and flows out from the outlet pipe 17.

FIG. 3 is a cross-sectional view showing the state of the refrigerant R1 inside the flow divider 12, in which the flow pattern of the refrigerant R1 is almost all over from the inlet portion of the flow divider 12 by the ribbon-shaped turbulence promoting body 18. Cross over to the floss style.

Therefore, the refrigerant R1 equally flows out to each heat transfer tube 13 and evaporates equally. Refrigerant R split in the flow divider 12
1 is a heat transfer tube 1 connected in a U shape without joining again
It vaporizes in 3 and reaches the confluencer 14. Shunt 1 at this time
The ratio of the liquid phase mass flow rate of the refrigerant R1 flowing out from the No. 2 is shown by the length of the arrow in FIG.

Further, by installing the flow divider 12 and the flow combiner 14 in parallel, all the air A1 passing through the heat exchanger 11 can be obtained.
In the row of the heat transfer tubes 13 on the upstream side, heat is exchanged with the refrigerant R1 in the initial stage of evaporation, and all the air A1 is cooled and passes through the heat exchanger 11.
Since 1 is equally cooled and dehumidified, the heat exchange efficiency is good. As described above, according to the present embodiment, the flow divider 12 and the confluencer 14 are provided.
And a heat transfer tube 13 in which a large number of fins 15 are arranged. Inside the flow divider 12, a ribbon-shaped turbulence promoting body 1 is provided.
8 is provided, the gas-liquid two-phase flow refrigerant R in the flow divider 12 is provided.
Heat transfer tube 13 joined to shunt 12 with 1 as floss flow
The heat can be efficiently exchanged over the entire surface of the heat exchanger 11 by diverting the water evenly and arranging the flow distributor 12 and the confluent device 14 in parallel, and a small-sized and high-performance heat exchanger can be realized.

A second embodiment of the present invention will be described below with reference to the drawings. FIG. 4 shows the entire heat exchanger of the second embodiment of the present invention, in which a plurality of heat transfer tubes 23 are provided in a cylindrical flow distributor 22 having both ends sealed by a heat exchanger. It is joined.

Further, a plurality of heat transfer tubes 13 provided with a large number of fins 25 are also installed and joined in two rows in the confluence unit 24 arranged in parallel. The heat transfer tube 23 joined to the flow distributor 22 is appropriately connected in a U shape to form a circuit of the refrigerant R2.
An inlet pipe 26 is joined to the flow distributor 22 and an outlet pipe 27 is joined to the combiner 23. A ribbon-shaped turbulence promoting body 18 shown in FIG. 2 is provided only in the lower part inside the flow distributor 22.

The operation of the heat exchanger 21 configured as described above will be described below with reference to FIGS. 4 and 5.

The refrigerant R2 of a gas-liquid two-phase flow having a low degree of dryness sequentially flows out to the heat transfer pipe 23 while flowing upward in the flow divider 22 flowing into the flow divider 22 from the inlet pipe 26. U as appropriate
The heat transfer tube 23 on the rear surface side of the heat exchanger 21 evaporates while exchanging heat with the air A2 flowing from the entire surface on the side of the flow distributor 22 via the fins 25 arranged on the heat transfer tube 23 connected in a letter shape.
After it becomes dry steam, it reaches the merger 24, merges, and flows out from the outlet pipe 27.

FIG. 5 is a cross-sectional view showing the state of the refrigerant R2 inside the flow divider 22. At this time, the refrigerant R2 is caused by the ribbon-like turbulence promoting member 18 so that the flow pattern in the lower portion of the flow divider 22 changes from the annular spray flow. It shifts to the floss flow, and shifts to the floss flow over almost the entire area of the flow divider 22.

Therefore, the refrigerant R2 equally flows out to each heat transfer pipe 23 and evaporates equally. Refrigerant R split in the flow divider 22
2 is a heat transfer tube 2 connected in a U shape without joining again
It vaporizes in 3 and reaches the confluencer 24. Shunt 2 at this time
The ratio of the liquid phase mass flow rate of the refrigerant R2 flowing out from the No. 2 is shown by the length of the arrow in FIG.

Further, by installing the flow divider 22 and the combiner 24 in parallel, all the air A2 passing through the heat exchanger 21 can be obtained.
In the row of the heat transfer tubes 23 on the upstream side, heat is exchanged with the refrigerant R2 in the initial stage of evaporation, and all the air A2 is cooled and passes through the heat exchanger 21, so that the air A on the entire surface of the heat exchanger 21 is cooled.
Since 2 is equally cooled and dehumidified, the ribbon-shaped turbulence promoting body 18 is provided only in the lower part of the flow divider 22 where the effect is most prominent in this embodiment, which has good heat exchange efficiency, and the cost performance is improved. Can be significantly improved.

As described above, according to this embodiment, the shunt 2
2, a confluence device 24, and a heat transfer tube 23 in which a large number of fins 25 are arranged. Inside the flow distributor 22, a ribbon-shaped turbulence promoting body 18 is provided only in the lower portion, so that the flow distributor 2
The gas-liquid two-phase refrigerant R2 in 2 is turned into a froth flow and the flow divider 2
The heat transfer tube 23 joined to the 2 is divided evenly, and the flow divider 2
By arranging 2 and the confluencer 24 in parallel, heat can be efficiently exchanged over the entire surface of the heat exchanger 21, and a compact and high-performance heat exchanger can be realized.

FIG. 6 shows the entire heat exchanger according to the third embodiment of the present invention. Reference numeral 31 is a heat exchanger, and a plurality of heat exchangers are provided in a cylindrical flow divider 32 whose both ends are sealed. The heat transfer tube 33 is joined. Further, a plurality of heat transfer tubes 33 having a large number of fins 35 are also installed and joined in two rows in the confluence unit 34 arranged in parallel. The heat transfer tube 33 joined to the flow divider 32 is appropriately connected in a U shape to form a circuit of the refrigerant R3. An inlet pipe 36 is joined to the flow distributor 32, and an outlet pipe 37 is joined to the combiner 33. Inside the flow distributor 32, a ribbon-shaped turbulence promoting body 38 having small holes shown in FIG. 7 is provided.

The operation of the heat exchanger 31 configured as described above will be described below with reference to FIGS. 6 and 8.

The gas-liquid two-phase refrigerant R3 having a low degree of dryness sequentially flows out to the heat transfer tube 33 while flowing upward in the flow distributor 32 flowing into the flow distributor 32 from the inlet pipe 36. U as appropriate
The heat transfer tube 33 on the rear surface side of the heat exchanger 31 evaporates while exchanging heat with the air A3 flowing in from the entire surface on the side of the flow divider 32 via the fins 35 arranged on the heat transfer tube 33 connected in a letter shape.
After it becomes dry steam, it reaches the merger 34, merges, and flows out from the outlet pipe 37.

FIG. 8 is a cross-sectional view showing the state of the refrigerant R3 inside the flow divider 32. At this time, the refrigerant R3 is caused by the ribbon-shaped turbulence promoting body 38 so that the flow pattern of the lower portion of the flow divider 32 is changed from the annular spray flow. It shifts to the floss flow, and shifts to the froth flow almost all over the inside of the flow divider 32. At this time, the refrigerant R3 that passes through the small holes 39 and the refrigerant R3 that does not pass through are mixed well.

Therefore, the refrigerant R3 uniformly flows out to each heat transfer tube 33 and evaporates equally. Refrigerant R split in the flow divider 32
3 is a heat transfer tube 3 connected in a U shape without joining again
It vaporizes in 3 and reaches the confluencer 34. Shunt 2 at this time
The ratio of the liquid phase mass flow rate of the refrigerant R2 flowing out from the No. 3 is shown by the length of the arrow in FIG.

Further, by installing the flow divider 32 and the combiner 34 in parallel, all the air 32 passing through the heat exchanger 31 can be obtained.
In the row of the heat transfer tubes 33 on the upstream side, heat is exchanged with the refrigerant R3 in the initial stage of evaporation, and all the air 32 is cooled and passes through the heat exchanger 31.
Since 3 is equally cooled and dehumidified, in this embodiment, which has good heat exchange efficiency, the ribbon-like turbulence promoting body 38 is provided with the small holes 39, so that the mixing effect of the refrigerant and the pressure loss in the pipe are reduced. The performance can be significantly improved.

As described above, according to this embodiment, the flow divider 3
2, a confluence device 34, and a heat transfer tube 33 having a large number of fins 35 arranged therein.
By providing the ribbon-like turbulent flow promoting body 38 having the above, the gas-liquid two-phase flow of the refrigerant R3 in the flow divider 32 is evenly mixed and made into a floss flow, and the pressure loss in the pipe is kept low and bonded to the flow device 32. It is possible to efficiently perform heat exchange on the entire surface of the heat exchanger 31 by distributing the heat evenly to the heat transfer tube 33, and installing the flow distributor 32 and the combiner 34 in parallel. Can be realized.

[0045]

As described above, according to the present invention, a tubular flow distributor whose both ends are sealed, a tubular flow distributor whose both ends are sealed, and a substantially right angle to the flow distributor and the merger. And a plurality of heat transfer fins disposed on the heat transfer tube, and a turbulence promoting body is provided inside the flow divider, and the liquid refrigerant is a flow divider. It flows out almost evenly into the heat transfer pipes connected to and heat is exchanged efficiently.

Further, according to the present invention, a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, a plurality of the flow distributors, and a plurality of the flow joiners which are joined at substantially right angles to the flow combiner. A heat transfer tube and a plurality of heat transfer fins arranged on the heat transfer tube,
The flow distributor has a structure in which a ribbon-shaped turbulence promoting body is provided, and the turbulent flow promoting body has a ribbon shape, and the annular spray flow efficiently transfers to the froth flow and the liquid refrigerant is connected to the flow distributor. It flows out almost uniformly to all the heat transfer tubes, and heat exchange is efficiently performed.

Further, according to the present invention, a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, a plurality of the flow distributors and a plurality of the flow joiners which are joined at substantially right angles to the flow combiner. A heat transfer tube and a plurality of heat transfer fins arranged on the heat transfer tube,
The inside of the flow distributor is provided with a ribbon-shaped turbulence promoting body provided in almost the entire area from the lower part to the upper part of the flow distributor. Mixing of the refrigerant is promoted also in the floss flow region, and the liquid refrigerant flows out to all the heat transfer pipes connected to the flow distributor almost evenly, and heat exchange is efficiently performed.

Further, according to the present invention, a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, and a plurality of the flow distributors and a plurality of the flow joiners which are joined at substantially right angles to the flow combiner. A heat transfer tube and a plurality of heat transfer fins arranged on the heat transfer tube,
It is provided with a structure in which a ribbon-shaped turbulence promoting body is provided only inside the flow distributor inside the flow distributor, and the portion of the annular spray flow is effectively transferred to the floss flow, and the liquid refrigerant is , Evenly flows out to all heat transfer tubes connected to the shunt,
In all the heat transfer tubes, evaporation is similarly performed, and heat exchange is efficiently performed.

Further, according to the present invention, a tubular flow distributor whose both ends are sealed, a tubular flow combiner whose both ends are sealed, and a plurality of the flow distributors and a plurality of the flow joiners which are joined at substantially right angles to the flow combiner. A heat transfer tube and a plurality of heat transfer fins arranged on the heat transfer tube,
It is provided with a structure in which a turbulent flow promoting body having a small hole is provided inside the flow divider, and a portion of the annular spray flow moves to a froth flow, and a refrigerant passing through the small hole and a refrigerant not passing through the small hole are provided. The liquid refrigerant mixed and uniformly flows out to all the heat transfer tubes connected to the flow divider, the pressure loss in the tubes can be reduced, and the performance can be greatly improved.

[Brief description of drawings]

FIG. 1 is a perspective view of a heat exchanger according to a first embodiment of the present invention.

FIG. 2 is a perspective view of a turbulent flow promoting body of the heat exchanger.

FIG. 3 is a sectional view of a main part of the heat exchanger.

FIG. 4 is a perspective view of a heat exchanger according to a second embodiment of the present invention.

FIG. 5 is a cross-sectional view of the main parts of the heat exchanger.

FIG. 6 is a perspective view of a heat exchanger according to a third embodiment of the present invention.

FIG. 7 is a perspective view of a turbulent flow promoting body of the heat exchanger.

FIG. 8 is a sectional view of the main part of the heat exchanger.

FIG. 9 is a perspective view of a conventional heat exchanger.

FIG. 10 is a sectional view of a main part of the heat exchanger.

FIG. 11 is a sectional view of a main part of the heat exchanger.

[Fig. 12] Flow pattern diagram of vertical upward flow

FIG. 13 is a characteristic diagram explaining the flow pattern.

[Explanation of symbols]

 11,21,31 Heat exchanger 12,22,32 Flow divider 13,23,33 Heat transfer tube 14,24,34 Combiner 15,25,35 Fin 18,38 Turbulence accelerator 39 Small hole

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Teruhiko Hira 3-22 Takada Hon-dori, Higashi-Osaka City, Osaka Prefecture Matsushita Cold Machinery Co., Ltd.

Claims (5)

[Claims] 1. A tubular flow distributor with both ends sealed, a tubular combiner with both ends sealed, and a plurality of heat transfer tubes joined to the flow distributor and the combiner at substantially right angles. And a plurality of heat transfer fins arranged in the heat transfer tube, wherein a turbulent flow promoting body is provided inside the flow distributor. 2. A tubular flow distributor with both ends sealed, a tubular combiner with both ends sealed, the flow distributor, and a plurality of heat transfer tubes joined to the combiner at substantially right angles. A heat exchanger comprising a large number of heat transfer fins arranged in the heat transfer tube, wherein a ribbon-shaped turbulence promoting body is provided inside the flow distributor. 3. A tubular flow distributor whose both ends are sealed, a tubular combiner whose both ends are sealed, and a plurality of heat transfer tubes which are joined to said flow distributor and said combiner at substantially right angles. A heat exchanger comprising a large number of heat transfer fins arranged in the heat transfer tube, wherein a ribbon-shaped turbulence promoting body is provided inside the flow distributor over substantially the entire area from the lower part to the upper part of the flow distributor. 4. A tubular flow distributor whose both ends are sealed, a tubular merger whose both ends are sealed, and a plurality of heat transfer tubes which are joined to said flow distributor and said merger at substantially right angles. A heat exchanger comprising a large number of heat transfer fins arranged in the heat transfer tube, wherein a ribbon-shaped turbulent flow promoting body is provided inside the flow distributor only below the flow distributor. 5. A tubular flow distributor whose both ends are sealed, a tubular merger whose both ends are sealed, and a plurality of heat transfer tubes which are joined to said flow distributor and said merger at substantially right angles. A heat exchanger comprising a large number of heat transfer fins arranged in the heat transfer tube, wherein a turbulent flow promoting body having small holes is provided inside the flow distributor.